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CN113906002A - Method and system for removing light ends and non-condensables to prevent build-up in olefin/paraffin membrane separation processes - Google Patents

Method and system for removing light ends and non-condensables to prevent build-up in olefin/paraffin membrane separation processes Download PDF

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CN113906002A
CN113906002A CN202080040048.9A CN202080040048A CN113906002A CN 113906002 A CN113906002 A CN 113906002A CN 202080040048 A CN202080040048 A CN 202080040048A CN 113906002 A CN113906002 A CN 113906002A
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hydrocarbons
stripper
hydrogen
gas
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M·辛格
查尔斯·P·利布基
范忠
史蒂文·科祖普
卡尔·里斯基
西蒙·E·阿尔博
莎迪特·乌拉斯·阿基戈兹
刘春庆
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Honeywell UOP LLC
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/06—Propene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/144—Purification; Separation; Use of additives using membranes, e.g. selective permeation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/64—Propane or propylene

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  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

本发明提供了用于防止轻馏分诸如甲烷、乙烯和乙烷在烯烃/链烷烃分离系统中积聚的系统和方法，所述烯烃/链烷烃分离系统使用膜和蒸馏塔的组合以用于该分离。在一个实施方案中，在选择性加氢反应器下游提供小型汽提器塔。在另一个实施方案中，向膜单元的滞留物料流添加具有接收器的调压容器。

Figure 202080040048

The present invention provides systems and methods for preventing the accumulation of light ends such as methane, ethylene, and ethane in olefin/paraffin separation systems that use a combination of membranes and distillation columns for the separation . In one embodiment, a small stripper column is provided downstream of the selective hydrogenation reactor. In another embodiment, a surge vessel with a receiver is added to the retentate stream of the membrane unit.

Figure 202080040048

Description

Method and system for removing light ends and non-condensables to prevent buildup in an olefin/paraffin membrane separation process
Technical Field
The present disclosure relates generally to methods and systems for separating olefins and paraffins in a membrane system. More specifically, the present disclosure relates to a method of preventing light ends from accumulating in a propylene stream.
Background
Membrane-bound processes have been developed for purifying streams comprising mixtures of propane and propylene. It has been found that the gas mixture to these membranes contains light ends including hydrogen, methane, ethane and ethylene. These light ends are a problem because they can accumulate in the system and degrade the performance of the upper compressor or membrane without meeting product specifications.
Among the processes for producing propylene is fluid catalytic cracking, which produces naphtha and crude liquid products as well as lighter hydrocarbons and hydrogen. Lighter hydrocarbons may be subjected to various treatments including removal of sulfur compounds by processes such as UOP's Merox process to oxidize mercaptan compounds and sending through a C3/C4 separator to remove C4 hydrocarbons from the C3/C4 stream and a C3 separator (distillation column to remove propane). In the prior art process, a deethanizer column is used to remove and recycle C2.
In a typical prior art FCC process, after the process products (including the heavy naphtha product, the light cycle oil product, and the heavy oil product) are produced, there is a vapor stream containing some lighter hydrocarbons and unstable gasoline. The gasoline is removed for processing as fuel gas as such. There are C3 and C4 hydrocarbons that are sent for further processing, including alkylation or polymerization and mercaptan removal processes such as UOP's Merox processes. After mercaptan removal, in a typical plant, the stream is sent to a C3/C4 separator to recover C4 hydrocarbons, then C2 hydrocarbons are removed by a deethanizer (as part of the tail gas stream) and recycled to the gas concentration unit. The stream is then sent to a C3 separator to separate propylene and propane.
Disclosure of Invention
In one embodiment, the invention is a process for removing hydrogen and lighter hydrocarbons from a hydrocarbon stream, the process comprising: passing a gas stream comprising hydrogen and C1-C3 hydrocarbons to a stripper column to produce a stripper tail gas stream from a top section of the stripper column and a bottom stream comprising C3 hydrocarbons, the bottom stream being passed through a C3 separator to produce a second bottom stream comprising propane and a second overhead stream comprising propylene; sending the second overhead stream through a membrane unit to produce a permeate stream comprising a higher concentration of propylene than the second overhead stream and a retentate stream comprising a higher concentration of propane than the second overhead stream; and returning the retentate stream to the C3 separator.
Another embodiment of the invention is a process for removing lighter hydrocarbons from a gas stream, the process comprising: sending a gas stream comprising C1 to C3 hydrocarbons to a membrane unit to produce a propylene permeate stream and a retentate stream comprising C1 to C3 hydrocarbons; sending the retentate stream to a surge vessel to separate the retentate stream into a propane stream and a surge vessel tail gas stream comprising C1 to C2 hydrocarbons; and sending the pressure regulated vessel tail gas stream to a gas concentration unit.
Drawings
Figure 1 shows a flow diagram with added stripper column.
Figure 2 shows a flow chart with an added surge vessel.
Detailed Description
In the present invention, there are two alternative processes for removing light ends from a propylene stream. The first method is to remove the selective hydrogenation reactor by providing a small stripper column after them. A second method is to remove the light fraction leaving the retentate by providing a surge vessel with a packing section for efficient separation.
In existing plants, in the absence of an existing deethanizer that removes C2 and lighter components and returns them to the gas concentration unit, a small stripper column must be included to manage the light ends and non-condensables of the effluent exiting the KLP reactor. The KLP process is a hydrogenation process for converting acetylene compounds to olefins. Light ends (if not removed) can accumulate in the upper portion of the C3 separator and can cause several problems: decreasing compressor performance, increasing/accumulating concentrations over time without outlet (although light olefins, ethylene can permeate with C3), and decreasing product purity. The stripper can be operated at 2170-. The stripper can also be a column with high efficiency and lower HETP (theoretical equivalent plate height) packing (with random/structured packing) with 5 to 25 theoretical plates, or preferably 8 to 22 theoretical plates. At this operating pressure, the upper condensing temperature is 37.8-65.6 deg.C (100 deg.F.) or preferably 43.3-60 deg.C (110 deg.F.) which can be cooled with supply of air or cooling water. Hydrogen and methane may be completely removed in the upper portion of the stripper, while C2 hydrocarbons may be removed up to 80-100%, or preferably 90-99%. The concentration of C2 in the stripper bottoms stream is from 0 to 30wt ppm, or preferably from 2 to 25wt ppm.
A second method of removing light ends in the present invention without using a stripper column is to install a surge vessel with a receiver on the retentate stream of the membrane. Light end components such as methane and ethane are not permeable but remain with the propane. However, if there is no outlet, these components can easily accumulate in this stream due to the recirculation loop back to the column. Thus, having the surge vessel set at a temperature provides an outlet for these components and prevents them from accumulating in the system. Note that any C3 that is discharged in the vent stream with C1 and C2 may be directed back to the gas concentration unit for further C3 recovery (same as deethanizer tail gas and stripper tail gas treatment). The surge vessel is a receiver having a dewatering guide zone and a vertical discharge section at the top. The vertical discharge section is a loading section/chimney having a height of 0.6-6.1m (2-20ft) or preferably 1.2-3.7m (4-12ft), a diameter of 0.30-1.5m (1-5ft) or preferably 0.3-0.9(1-3 ft). The top of the vertical section, 0.3-3.0m (1-10ft), or preferably 0.61-2.4m (2-8ft), is cooled with a refrigerant to remain at 7.2-21.1 ℃ (45-70 ° F), preferably 12.8-18.3 ℃ (55-65 ° F). The refrigerant can be an external refrigerant or an internal process fluid (propylene product) that can be recycled and recompressed and cooled to meet the required cooling load. In the case of a pressure-regulated vessel, the total ethane removal is 85-99%, preferably 90-98%. Note that if the acetylene hydrogenation reactor effluent has more than 100vol ppm ethylene, the first configuration using a stripper is preferred over the vent stripper due to the fact that ethylene can permeate through the membrane with C3 ═ C. The vent stripper can effectively remove ethane even if the acetylene hydrogenation reactor effluent has at most 2800mol ppm ethane (or 0.28% molar C2 concentration). The vent stripper may also remove any water in the retentate and accumulate it by in the lead section of the plant. The off gas from the surge vessel has a molar concentration of 0.1-20% C2, or preferably 0.5-10% C2, and can be directed to a gas concentration unit to recover the C3 component. The proposed configuration can be changed in order or applied in various ways by the person skilled in the art. The two configurations with a stripper will be combined after the vent stripper on the KLP reactor and retentate stream for a viable combination.
One solution is shown in fig. 1, in which a stripper 164 is shown after selective hydrogenation reactor 158. In fig. 1, a fresh hydrocarbon feed 126 is shown being sent to a fluid catalytic cracking reactor 120(FCC) where it is processed according to methods well known in the art. The regenerator 114 is located after the reactor 120, where air 112 enters with spent catalyst 122. The catalyst is regenerated and returned to the reactor 120 via line 124. Flue gas stream 116 is shown exiting the top of regenerator 114. Stream 128 exits the top of reactor 120 and is sent to main separator column 130 for separation into heavy cycle oil product 134, light cycle oil product 136, and heavy naphtha product 138. An upper stream 132 comprising a mixture of hydrocarbons, hydrogen, and unstabilized gasoline exits the top portion of the main separation column 130 and is sent to a gas concentration unit 140. The fuel gas stream 146, the debutanized gasoline stream 142, and the hydrocarbon stream 144 comprising C1 to C4 hydrocarbons are sent to a unit 148 to remove mercaptans, producing a stream 150, which is then shown to be sent to a C3/C4 separator 152, where a C4 bottoms stream 154 is sent to storage and a vapor overhead stream 156 is sent for further processing (shown as a processor 158 including a selective hydrogenation reactor where acetylene is reacted with hydrogen 159). Stream 160 is then sent to a stripper column 164 to produce a lighter tail gas stream 162 and a bottoms stream 166, which is then sent to a C3 separator 168 to produce a propane stream 170 that can be sent to a storage device (not shown) and a lighter stream 172 that is sent to a membrane unit 174. The retentate stream 176 is returned to the C3 separator 168 while the permeate stream 177 is sent to the compressor/dryer 180 to produce the propylene stream 182.
Figure 2 illustrates a solution in which a pressure regulated vessel 290 is shown to process the retentate 276 from the membrane unit 274. In fig. 2, a fresh hydrocarbon feed 226 is shown being sent to a fluid catalytic cracking reactor 220(FCC) where it is processed according to methods well known in the art. The regenerator 214 is located after the reactor 220, where air 212 enters along with spent catalyst 222. The catalyst is regenerated and returned to reactor 220 via line 224. Flue gas stream 216 is shown exiting the top of regenerator 214. Stream 228 exits the top of reactor 220 and is sent to main separation column 230 for separation into heavy cycle oil product 234, light cycle oil product 236, and heavy naphtha product 238. An upper stream 232 comprising a mixture of hydrocarbons, hydrogen, and unstabilized gasoline exits the top portion of the main separation column 230 and is sent to a gas concentration unit 240. A fuel gas stream 246, a debutanized gasoline stream 242, and a hydrocarbon stream 244 comprising C1 to C4 hydrocarbons are sent to unit 248 to remove mercaptans, producing stream 250, which is then shown to be sent to a C3/C4 separator 252, where a C4 bottoms stream 254 is sent to storage and a vapor overhead stream 256 is sent for further processing (shown as processor 258, which includes a selective hydrogenation reactor where acetylene is reacted with hydrogen 259). Stream 260 is then sent to a C3 separator 268 to produce a propane stream 270 that can be sent to a storage device (not shown) and a lighter stream 272 that is sent to a membrane unit 274. The retentate stream 276 is returned to the C3 separator 268 while the permeate stream 277 is sent to a compressor/dryer 280 to produce a propylene stream 282. A pressure regulating vessel 290 is shown through which a retentate gas stream 276 is passed, which is first cooled by a cooler 275, with most of the liquid sent to the C3 separator 268 through line 294, and water exiting at 296 and optionally recycled to the lighter stream 272 to provide this stream with the appropriate humidity level to enter the membrane unit 274. The exhaust tail gas stream 262 is returned to the gas concentration unit 240. Also shown is an inlet 292 for a refrigerant stream, such as propane refrigerant, for entering pressure regulating vessel 290 having refrigerant stream 293 exiting pressure regulating vessel 290.
Detailed description of the preferred embodiments
While the following is described in conjunction with specific embodiments, it is to be understood that this description is intended to illustrate and not limit the scope of the foregoing description and the appended claims.
A first embodiment of the invention is a process for removing hydrogen and lighter hydrocarbons from a gas stream, the process comprising: passing a gas stream comprising hydrogen and C1-C3 hydrocarbons to a stripper column to produce a stripper tail gas stream from a top section of the stripper column and a bottom stream comprising C3 hydrocarbons, the bottom stream being passed through a C3 separator to produce a second bottom stream comprising propane and a second overhead stream comprising propylene; sending the second overhead stream through a membrane unit to produce a permeate stream comprising a higher concentration of propylene than the second overhead stream and a retentate stream comprising a higher concentration of propane than the second overhead stream; and returning the retentate stream to the C3 separator. An embodiment of the invention is one, any or all of the first embodiment in this paragraph up through the previous embodiments in this paragraph wherein the stripper column is operated at a pressure of 2170-. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the stripper column comprises from 10 to 30 trays and preferably from 15 to 25 trays. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the stripper column is packed with packing and comprises 5 to 25 theoretical plates, preferably 8 to 22 theoretical plates. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein 100 wt% of the hydrogen and methane and 80 to 100 wt% of the C2 hydrocarbons are removed in the stripper column and sent to a gas concentration unit in an upper stream. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the stripper bottoms stream comprises from 0 to 30wt ppm C2 hydrocarbons. One embodiment of the invention isThe first embodiment in this paragraph up through one, any or all of prior embodiments in this paragraph, wherein the hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons comprises from 0 to 10 mole% hydrogen and preferably from 0 to 2 mole% hydrogen. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons comprises 0 to 10 mol% methane, preferably 0 to 2 mol% methane and 0 to 10 mol% C2 hydrocarbons, preferably 0 to 5 mol% C2 hydrocarbons. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons is monitored by an analyzer and an on-line system to monitor and measure H2、CH4And C2The hydrocarbon concentration. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the stripper tail gas stream is in communication with the upper condenser and the vent condenser. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the vent condenser vapor outlet stream comprises from 0 to 10 mole% hydrogen, preferably from 0 to 5 mole% hydrogen and from 0 to 50 mole% C2 hydrocarbon or preferably from 0 to 35 mole% hydrocarbon. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the vent condenser vapor is directed to a fuel gas system, vented or directed to a gas concentration unit where ethylene and propylene are recovered. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the vent condenser vapor is fully condensed wherein no condensable gases are detected in the feed stream to the stripper column. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the first and second regions are formed by a chemical vapor deposition processA feed stream is bypassed to the stripper column to operate the stripper column in direct communication with the C3 splitter column.
A second embodiment of the invention is a process for removing hydrogen and lighter hydrocarbons from a gas stream, the process comprising: sending a gas stream comprising C1 to C3 hydrocarbons to a membrane unit to produce a propylene permeate stream and a retentate stream comprising C1 to C3 hydrocarbons; sending the retentate stream to a surge vessel to separate the retentate stream into a propane stream and a surge vessel tail gas stream comprising C1 to C2 hydrocarbons; and sending the pressure regulated vessel tail gas stream to a gas concentration unit. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the pressure regulating vessel is a receiver having a dewatering guide section and a vertical discharge section at a top section of the pressure regulating vessel. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the vertical discharge section is a priming section having a height of 0.6 to 6.1m and preferably 0.3 to 0.9 m. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the top section of the surge vessel is cooled to 7.2 to 21.1 ℃. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through this paragraph wherein the pressure regulating vessel tail gas stream comprises from 0.5 to 10 mol% C2 hydrocarbons. An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein a total of from 85 to 99 weight percent of the ethane is removed.
Without further elaboration, it is believed that one skilled in the art can, using the preceding description, utilize the present invention to its fullest extent and can readily ascertain the essential characteristics of the present invention without departing from the spirit and scope thereof, to make various changes and modifications of the invention and to adapt it to various usages and conditions. Accordingly, the foregoing preferred specific embodiments are to be construed as merely illustrative, and not limitative of the remainder of the disclosure in any way whatsoever, and is intended to cover various modifications and equivalent arrangements included within the scope of the appended claims.
In the foregoing, all temperatures are shown in degrees celsius and all parts and percentages are by weight unless otherwise indicated.

Claims (10)

1.一种从烃料流中去除氢气和较轻烃的方法，所述方法包括：1. A method of removing hydrogen and lighter hydrocarbons from a hydrocarbon stream, the method comprising: a.将包含氢气和C1-C3烃的烃料流传送到汽提器塔，以产生来自所述汽提塔的顶部区段的汽提器尾气料流和包含C3烃的底部料流.a. Passing a hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons to a stripper column to produce a stripper off-gas stream from the top section of the stripper column and a bottoms stream comprising C3 hydrocarbons. b.将所述底部料流传送通过C3分离器，以产生包含丙烷的第二底部料流和包含丙烯的第二顶部料流；b. passing the bottoms stream through a C3 splitter to produce a second bottoms stream comprising propane and a second overhead stream comprising propylene; c.将所述第二顶部料流发送通过膜单元，以产生渗透物料流和滞留物料流，所述渗透物料流包含比所述第二顶部料流更高浓度的丙烯，所述滞留物料流包含比所述第二顶部料流更高浓度的丙烷；以及c. Sending the second overhead stream through a membrane unit to produce a permeate stream comprising a higher concentration of propylene than the second overhead stream and a retentate stream, the retentate stream contains a higher concentration of propane than the second overhead stream; and d.使所述滞留物料流返回到所述C3分离器。d. Return the retentate stream to the C3 separator. 2.根据权利要求1所述的方法，其中所述汽提器塔在2170-3204kPa(300-450)psig压力的压力下操作。2. The method of claim 1, wherein the stripper column operates at a pressure of 2170-3204 kPa (300-450) psig pressure. 3.根据权利要求1所述的方法，其中100重量％的氢气和甲烷以及80-100重量％的C2烃在所述汽提塔中被去除，并且在上部料流中被发送到气体浓缩单元。3. The method of claim 1 wherein 100 wt% hydrogen and methane and 80-100 wt% C2 hydrocarbons are removed in the stripper and sent to a gas concentration unit in an upper stream . 4.根据权利要求1所述的方法，其中汽提器底部料流包含0-30wt ppmC2烃。4. The method of claim 1 wherein the stripper bottoms stream comprises 0-30 wt ppm C2 hydrocarbons. 5.根据权利要求1所述的方法，其中所述包含氢气和C1-C3烃的烃料流包含0-10摩尔％甲烷和0-10摩尔％C2烃。5. The method of claim 1, wherein the hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons comprises 0-10 mole % methane and 0-10 mole % C2 hydrocarbons. 6.根据权利要求1所述的方法，其中通过分析仪和在线系统来监测所述包含氢气和C1-C3烃的烃料流，以监测和测量H2、CH4和C2烃浓度。6. The method of claim 1, wherein the hydrocarbon stream comprising hydrogen and C1-C3 hydrocarbons is monitored by an analyzer and an on-line system to monitor and measure H2, CH4 and C2 hydrocarbon concentrations. 7.根据权利要求1所述的方法，其中所述汽提器尾气料流与上部冷凝器和排放冷凝器连通。7. The method of claim 1, wherein the stripper off-gas stream is in communication with an upper condenser and a vent condenser. 8.根据权利要求7所述的方法，其中排放冷凝器蒸气出口料流包含0-10摩尔％氢气和0-50摩尔％C2烃。8. The method of claim 7, wherein the vent condenser vapor outlet stream comprises 0-10 mole % hydrogen and 0-50 mole % C2 hydrocarbons. 9.根据权利要求8所述的方法，其中所述排放冷凝器蒸气被引导到燃气系统，被排放或引导到其中回收乙烯和丙烯的气体浓缩单元。9. The method of claim 8, wherein the vent condenser vapor is directed to a gas fired system, vented or directed to a gas concentration unit in which ethylene and propylene are recovered. 10.根据权利要求9所述的方法，其中所述排放冷凝器蒸气完全冷凝，其中在送至所述汽提器塔的进料料流中没有检测到可凝性气体。10. The process of claim 9, wherein the vent condenser vapor is fully condensed, wherein no condensable gas is detected in the feed stream to the stripper column.
CN202080040048.9A 2019-05-29 2020-05-26 Method and system for removing light ends and non-condensables to prevent build-up in olefin/paraffin membrane separation processes Pending CN113906002A (en)

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